Process for the manufacture of chrome chemicals

ABSTRACT

Chrome chemicals such as chromic acid (CrO3) and alkali metal chromates and bichromates are prepared by a process which avoids the formation and treatment of &#39;&#39;&#39;&#39;brown muds&#39;&#39;&#39;&#39; which includes the processing steps of reacting an alkali metal bisulfate solution substantially free of trivalent chromium values with an aqueous solution of an alkaline roasted chrome ore mixture containing dissolved chrome ore values to convert the roasted mixture&#39;&#39;s chrome ore values at least in part to an alkali metal bichromate and separating said bichromate values. The alkali metal bichromate values may be reacted with a sulfuric acid to produce chromic acid. Also covered by the present invention is the removal of the chloride impurity from the bichromate values.

United States Patent [1 1 Morgan et a1.

[54] PROCESS FOR THE MANUFACTURE OF CHROME CHEMICALS [75] Inventors: Thomas R. Morgan; William W. Low, both of Syracuse; Christian A. Wamser, Camillus; Charles P. Bruen, Fayetteville, all of N.Y.

[73] Assignee: Allied Chemical Corporation, New

York, N.Y.

[22] Filed: Oct. 19, 1970 [21] Appl. No.: 82,024

[51] Int. Cl. ..C0lg 37/14 [58] Field of Search ..23/56, 145; 204/82; 423/61,

[56] References Cited UNITED STATES PATENTS 2,639,216 5/1953 Banner ..23/56 1,924,710 8/1933 Demant ..23/56 2,839,359 6/1958 Dunning ..23/56 51 Feb. 6, 1973 4 Primary Examiner-Herbert T. Carter Attorney-Gerard P. Rooney [57] ABSTRACT Chrome chemicals such as chromic acid (CrO and alkali metal chromates and bichromates are prepared by a process which avoids the formation and treatment of brown muds" which includes the processing steps of reacting an alkali metal bisulfate solution substantially free of trivalent chromium values with an aqueous solution of an alkaline roasted chrome ore mixture containing dissolved chrome ore values to convert the roasted mixtures chrome ore values at least in part to an alkali metal bichromate and separating said bichromate values. The alkali metal bichromate values may be reacted with a sulfuric acid to produce chromic acid. Also covered by the present invention is the removal of the chloride impurity from the bichromate values.

20 Claims, 1 Drawing Figure PATENTEUFEB s 1975 Cr(ll|) FREE No HSOL CHRW RoAsTms AND YELLOW Ll QUOR" "RED LIQUOR" Nu Cr M12304 \lr CHLORINE GAS MULTISTAGE EVAPORATOR BY-PRODUCT BY-PRODUCT No o M02304 FOR M12304 2 2 1 PRODUCT" M25208 FOR MARKET LIQUOR LECWOOLHYggi CELL ill /7\ Nuzcrzofl 2 H ""2 2 a CRYSTALLIZER 20 -6 E58; E A D /9 A R OLV R N RECRYSTALLIZER 2 85 "0 PRODUCT r L r 22..- NGZCI2 0 ANHYDROUS 7 "2 4 OR B|cHRoMATE/cHRo |c/24 OLEUM ACID CONVERSION J, L- '28 /3- BY-PRODUCT No H304 Cr 0 29 1 R No H804 Cr 0 PRODUCT -26 Cr (m) ofloAnou FOR MARKET 27 INVENTORS THOMAS R. MORGAN WILLIAM W. LOW

CHRISTIAN A. WAMSER PROCESS FOR THE MANUFACTURE OF CHROME CHEMICALS This invention relates to the production of hexavalent chromium compounds useful in the plating of metals, the tanning of leather, the manufacture of pigments, in chemical processing and in many other chemical processing industries. More particularly, this invention is directed to a process for the manufacture of chromic acid and-alkali metal chromates and bichromate, which process permits the recovery and reuse of acid values, the elimination of troublesome and costly processing steps and the removal of chloride contamination.

conventionally, alkali metal chromates, such as sodium chromate, which is a valuable product as well as the precursor for chromic acid, alkali metal bichromates, such as sodium bichromate, and other chromium compounds, are produced from chromite ore, such as FeOcr O usually by high temperature alkaline oxidation followed by water leaching to produce a yellow liquor which is a solution of sodium chromate contaminated with sodium chloride. This method of preparing a chrome-containing solution from which the chrome values may be separated is preferred over other routes, such as the more cumbersome process involving pressure digestion of the chromite ore with sulfuric acid, using chromic acid as a catalyst, and separation of the metals by means of the crystallization of complex double salts with ammonium sulfate. Such a process involves high costs and there is no by-product utilization.

BACKGROUND OF THE INVENTION In the past, it has been the practice to treat the crude chrome-containing solution (yellow liquor) with an acidic material, usually sulfuric acid, to form the socalled red liquor" which comprises a solution of alkali metal bichromate and by product alkali metal sulfate contaminated with chloride ion. Less frequently, carbon dioxide has been used rather than sulfuric acid as the acidic material, in which case alkali metal bicarbonate rather than alkali metal sulfate is obtained as by-product and is recycled to the chromite ore alkaline oxidation step.

Another variation of the prior art has been the use of by-product alkali metal bisulfate as the acidic material obtained from the production of chromic acid in place of sulfuric acid in the production of bichromate. The value of the bisulfate as a saleable by-product of chromic acid preparation has presented a problem to the manufacturers of chromic acid because of the presence of both trivalent and hexavalent chromium as well as chloride ions originally present in the alkali (soda ash) used in the chromite ore alkaline oxidation step. While the by-product bisulfate from the chromic acid process may be utilized in the production of bichromates, thus eliminating the problem of disposing of sodium bisulfate, unfortunately its use has introduced other problems which have become increasingly severe as the production rate of chromic acid has increased.

The presence of hexavalent chromium in the bisulfate presents no problem since it can be returned to the process, but the trivalent chromium, also present in significant amounts, causes precipitation of a complex mixture known in the trade as brown muds. These muds are somewhat gelatinous in character. As

deposited, filtration is almost impossible, but they can be filtered (with great difficulty) if sufficient water is added and if the pH is held at about 5. The additional water increases the filtration load and subsequently the evaporative load increasing capital and fuel costs. Thus, the treatment of the brown muds" represents a major filtration operation with attendant capital and operational costs. Furthermore, when the pH is not maintained in order to achieve filterability, conversion of the alkali metal chromate to bichromate is incomplete, and a further step is necessary to complete the conversion. If the muds are discarded after filtration, they represent a yield loss because of the chromi um values, both trivalent and hexavalent, contained therein. Attempts to recycle these muds back to the initial high temperature alkaline oxidation step to insure minimum loss of chrome values introduces further problems in the leaching and washing operation which follows.

Another problem encountered in methods of the prior art is the halide ion, particularly chloride ion, contamination of the working solutions and products. The major portion of the chloride contaminant is introduced by the alkali used in the initial high temperature oxidation of the chromite ore and subsequent crystallization of the sodium bichromate. To reduce loss of the chrome values recycling is employed; and as a result, the chloride ion in the mother liquor accumu-' lates to troublesome levels causing contamination of the final products. The chloride level, if not regulated andallowed to follow the product bichromate, could amount to as much as 0.5% Cl on a Na Cr Q -2H O basis. Such contamination adversely affects the performance of these compounds in pigments and electroplating operations, and often introduces serious corrosion problems during manufacture or utilization of these products. These halide ions must be removed one way or the other from the system. Various solutions to this problem are known to the art. For instance, employing a low chloride alkali will greatly diminish the problem, but add to the cost. The chloride ions can be removed from the working solutions by precipitation using silver ions (U.S. Pat. No. 2,639,216) or by electrolytic means (U.S. Pat. No. 3,454,478); these treatments, however, add to the cost of the chrome products produced.

In the prior art processes, the yellow liquor containing heavy traces of sodium chloride is acidified with an alkali metal bisulfate, preferably the by-product bisulfate resulting from the chromic acid conversion step, described hereinbelow. The acidity of the reaction mixture is kept below about 5 wherein conversion to sodium bichromate is incomplete and the reaction mixture contains sodium bichromate, unconverted sodium chromate, sodium sulfate, sodium chloride, and the difficultly filterably brown muds" comprising a complex containing trivalent chromium and hexavalent chromium values. The muds are removed by filtration, usually employing a silicious filter aid and either discarded or recycled to the initial chromite ore alkaline oxidation step. The filtrate is then treated with sulfuric acid to bring the pH to about 3.0, and the conversion of the remaining chromate to bichromate is completed. The resulting mixture is known in the trade as red liquor and comprises sodium bichromate, by-

product sodium sulfate having market value, and sodium chloride.

Generally, the red liquor is then concentrated in an evaporator and the concentrated solution treated for the removal of chloride ions by one of several methods described above.

The concentrated liquid emerging from the evaporator is essentially sodium bichromate which is separated from the by-product sodium sulfate by fractional crystallization, and crystallized from the purified solution, as Na,Cr '2H O product. The separated sodium sulfate called chrome cake" is a saleable by-product.

In an integrated system chromic acid is produced by taking a portion of the product sodium bichromate (Na Cr O1-2H2O) redissolved in an aqueous solution and recrystallized at a temperature above 85C. to provide the anhydrous product, Na Cr O The anhydrous sodium bichromate is then reacted with either sulfuric acid or oleum at about 200C. to produce chromic anhydride (CrO and sodium bisulfate (Nat-I80 At the reaction temperature employed, the products chromic anhydride and the by-product NaHSO,, exist essentially as immiscible liquid phases which are separated by conventional liquid/liquid separation techniques. However, during the above reaction the CrO undergoes some thermal decomposition resulting in the formation of the lower-valent trivalent chromium in the form of decomposition products which are transferred into the bisulfate phase. It is this bisulfate by-product, containing trivalent chromium decomposition products, that is recycled to react with the yellow liquor containing sodium chromate to form the red liquor and brown muds described hereinabove.

PRESENT INVENTION In accordance with the present invention, a new method is provided for producing chrome products which process avoids the production of brown muds and eliminates the need for foreign additives or additional steps to reduce the halide ion contamination.

As noted above, chromite ore, comprising essentially FeOCr O is roasted with an alkali metal carbonate, such as soda ash or potassium carbonate and other alkaline material as Ca() and MgO with the consequent formation of an alkali metal chromate. Conventional roasting temperatures normally employed are in the order of about 2,000 to 2,400F. The alkali metal chromate, preferably sodium, is then extracted from the calcined mixture to produce a yellow liquor comprising essentially an aqueous solution of the alkali metal chromate. While hereinafter specific reference will be made to the sodium salts, it is intended to cover the other alkali metal salts within the scope of the present invention.

FIG. 1 is a schematic representation of the preferred processing of chromite ores for the production of chrome values according to the present invention.

Of the various acidic materials that can be reacted with the yellow liquor in the production of the solution of sodium bichromate (red liquor), the present invention employs the by-product sodium bisulfate resulting from the preparation of chromic anhydride (Cr0 However, prior to the use of this by-product bisulfate, which contains traces of trivalent as well as hexavalent chromium, it is treated with sodium persulfate under oxidation conditions to convert essentially all of the trivalent chromium to hexavalent chromium preferably about 3 which is characteristic of a solution" containing bichromate and sulfate at the working concentration levels.

The red liquor comprising sodium bichromate sodium sulfate and traces of chloride prior to evaporation, is treated according to the method of the present invention so that the red liquor upon evaporation produces an essentially chloride-free sodium bichromate. To the red liquor is added an aqueous sodium persulfate solution, which preferably derived from the electrolytic oxidation of sodium bisulfate, described hereinbelow. The persulfate solution comprises a mixture of sodium bisulfate and sodium persulfate. This solution may be added to the red liquor either prior to, or during the evaporation step. The use of persulfate to remove chloride ion is found to be effective over a wide range of operating conditions. It is effective at essentially all degrees of acidity (pl-I 7), all bichromate concentrations varying from very dilute to saturated and all sulfate/bichromate concentration ratios up to approximately 2 mols Na SO per mol of Na Cr O,. This affords an effective and efficient method for removing the chloride ion in that the persulfate solution preferably is prepared from the by-product sodium sulfate and without the introduction of foreign ions into the system.

monly referred to as chrome cake is essentially pure and can be sold as is.

In the preferred embodiment of the present invention, a portion of this sodium sulfate by-product may be utilized for the production of sodium persulfate by electrolytic means. The resulting persulfate is then used as an oxidizing agent, described hereinabove, for the oxidation of the chloride ion in the red liquor prior to or during the evaporation step. Also, the persulfate can be employed to convert by oxidation the trivalentchromium values to hexavalent chromium values in the sodium bisulfate solution used to treat the yellow liquor.

To prepare sodium persulfate from the by-product sodium sulfate, sulfuric acid is first added in stoichiometric amounts to a solution of the sodium sulfate, preferably the by-product from the evaporators, to produce a solution of sodium bisulfate. Alternatively, the sodium bisulfate by-product from the manufacture of chromic anhydride may be used. The solution containing from about 40 to 60 percent NaHSO preferably from 50 to 60 percent, is oxidized by electrochemical means such as a diaphragm electrolytic cell to sodium persulfate. The operation of the electrolytic cell under optimum current efficiences are obtained employing high electrolyte concentration, high anode current density, anode materials of high oxygen overvoltage (such as platinum or platinized metals) and temperatures in the range of about 0-30C. The addition of small amounts of chloride ion increases the current efficiency. While the presence of the chloride ion in the process solution is normally avoided, the efficiency with which chloride may be removed by using the persulfate oxidation of it, as previously described, allows chloride addition at this point.

After the crystallization of the sodium bichromate, from which sodium sulfate has been separated by fractional crystallization, the hydrated bichromate crystals (Na Cr O1'2H2O) may be separated and stored. To prepare chromic anhydride (CrO the sodium bichromate is redissolved and recrystallized at a temperature in excess of 85C. to obtain the anhydrous bichromate, Na Cr OZ which is crystallized at temperatures between about 85 and 140C. The anhydrous bichromate is then treated with a sulfuric acid, such as concentrated sulfuric acid or preferably oleum, to produce chromic anhydride (CrO and by-product sodium bisulfate. This reaction is carried out at temperatures between about 196 and 210C., preferably at tempera tures between about 196 and 200C. At these temperatures, both the-product chromic anhydride (CrO and the by-product sodium bisulfate (NaHSO exist as essentially immiscible liquids which may be separated by conventional liquid/liquid phase separation techniques.

At these temperatures some of the molten CrO undergoes thermal decomposition and the resulting lower-valent chromium (trivalent chromium) decomposition products transfer into the bisulfate phase. As a result, the bisulfate normally contains some hexavalent chromium compounds (from dissolved or dispersed CrO not removed in the phase separation) and the trivalent chromium as well. If this byproduct sodium bisulfate were utilized as the acidic agent in the conversion of the sodium chromate in the yellow liquor to the sodium bichromate in the red liquor, described hereinabove, the hexavalent chromium values would be recovered and not interfere'with the conversion, but the trivalent chromium values would interfere with the conversion of the chromate to bichromate and these trivalent chromium values would be lost, as the difficultly filterable brown mud previously described.

In another aspect of the present process, this byproduct sodium bisulfate containing both hexavalent and trivalent chromium values is treated with sodium persulfate, preferably the sodium bisulfate-sodium persulfate mixture which was prepared by the electrochemical oxidation of sodium bisulfate in the electrolytic diaphragm cell, described above. The trivalent chromium is oxidized to hexavalent chromium according to the reaction:

The oxidationof the trivalent chromium is carried out in the aqueous phase, preferably on the nearly saturated sodium bisulfate used in the process. Substantially all, i.e., about percent, preferably about percent, of the trivalent chromium can be oxidized in 3 hours at 60C., using a stoichiometric quantity of the persulfate (Na S O that is, approximately 7 parts by weight of Na s O for every part of trivalent chromium [Cr(lll)]. The oxidation can be carried out at higher temperatures from 60Cfto the boiling point of the solution which is about C. As the temperature is increased, the time required for complete oxidation is likewise decreased. At 70C. the oxidation is found to be 90 percent complete in one hour. The reaction appears to be first-order with respect to trivalent chromium, with the rate of oxidation being proportional to the concentration of Cr(lll) in the solution. Using temperatures above about 70C. requires an increase in the amount of persulfate due to the thermal decomposition of the persulfate during the oxidation.

As with the chloride oxidation, one of the advantages of this method of Cr(lll) oxidation using process streams generated in the system is that no foreign ions are introduced into the system. Another is that the reaction generates acid which not only is utilizable in the subsequent chromate-bichromate conversion, but more than compensates for the acid values consumed in the production of the persulfate. Other methods of oxidizing the Cr(lll) in sodium bisulfate have been found less effective. For instance, the electrochemical oxidation of trito hexa-valent chromium in this medium proceeds with poor current efficiencies and requires the use of two-compartment cells with ion exchangemembrane separators to minimize cathodic reduction of the hexavalent chromium in the system. In the case of chemical oxidation by sodium chlorate, (NaCIO the reaction is so slow that even at the boiling point, as much as 16 hours may be required to oxidize most of the Cr(lll) with 200 percent excess of NaClO The by-product sodium bisulfate solution, in which substantially all of the trivalent chromium values have been converted to hexavalent chromium, can be used to convert the sodium chromate in the yellow liquor to sodium bichromate without dilution or final pH limitations and without precipitating brown muds. The conversion operation can be continued without interruption to the finishing pH which is characteristic of complete conversion (about 3.0-3.5). 1n the conversion, the by-product sodium bisulfate is added with agitation to the yellow liquor containing sodium chromate at a temperature of between 25 and C., preferably between 60 and 80C., to produce red liquor containing sodium bichromate. Some sodium sulfate crystallizes out because the system does not have the additional water otherwise needed to improve the properties of the brown mud" precipitate and facilitate filtration. The separation of the sodium sulfate along with traces of unoxidized trivalent chromium is easily achieved by centrifugation. This step desirably reduces the evaporative load in the subsequent processing of the red liquor. All that might be required for a final Cr(lll)-free red liquor feed for evaporation is a polishing filter which would be much smaller than the brown mud filtration system required in the conventional operation.

For a more complete understanding of the present invention, reference is made to the accompanying drawing in which:

FIG. 1 is a diagrammatic flow sheet of a chrome recovery process in which chrome ore 1 is subjected to a high temperature alkaline oxidation or roasting step, cooled and leached with an aqueous solution to produce the yellow liquor 2, comprising a solution of impure sodium chromate which is filtered to remove in soluble impurities from the roasted ore.

The yellow liquor is acidified with the sodium bisulfate solution which is substantially free of trivalent chromium salts. This can conveniently be carried out in a tank provided with a stirrer and the reaction is very rapid. As shown in the flow sheet, the resulting product is red liquor 4, comprising an aqueous solution of sodium bichromate, sodium sulfate and sodium chloride. Table l contains pertinent data on this conversion.

TABLE I Conversion, Na CrO, to Na Cr O Range Preferred Wt. percent of Na CrO, in leach liquor to 45 40 to 45 Cone. of by-product Nal-lSO solution 30 to 60 50 to 60 Liters NaHSO, soln. liters yellow liquor 0.2 to 1.4 0.5 to 0.8 Conversion temp. (C.) to 120 60to 80 pH of soln. 3.0 to 3.4 3.0 to 3.4

After filtration, this red liquor goes to a multiple effect evaporation system 5, together with a quantity of electrolytic cell liquor 6 produced in the electrolytic cell (11). The liquor contains a mixture of sodium bisulfate and sodium persulfate. The oxidation of the chloride ion can be carried out prior to or in conjunction with the concentration of the red liquor. Table ll presents pertinent data concerning the chloride ion oxidation.

TABLE ll Removal of Chloride Ion; Sepn. pf Na SO Range Preferred Liters cell liquor/liter of 0.02 to 0.1 0.02 to 0.05 red liquor" grams/liter (g/l) Na,S,0,, in 200 to 950 400 to 950 cell liquor gll NaHSO, in cell liquor 0 to 400 0 to 400 acid, then routed to electrolytic diaphragm cell 11. The main product from the evaporator 5 comprising a concentrated solution of sodium bichromate 15, is transferred to a heated holding tank 16 and then to a crystallizer l7. Crystals of Na Cr O -2H O are obtained as a final saleable product 18 and the liquors 19 are recirculated back to the evaporator S.

The by-product Na SO (10) to be electrolytically converted to sodium persulfate is approximately a 45 percent solution by weight based on Na SO While byproduct sodium bisulfate 13 from the production of chromic anhydride may be used as feed to the electrolytic cell, rather than the acidified sodium sulfate from the red liquor multistage evaporator, it is not preferred because of its heavier chromium contamination which may cause difficulty during electrolysis. To Na SO solution 10 is added approximately the stoichiometric amount of H 50, (12) required to produce a solution of sodium bisulfate, according to the reaction:

Na SO H,so, znanso,

The electrochemical oxidation of bisulfate to persulfate may be carried out in cells without diaphragms if the cathodes are wrapped with asbestos, or other non-reactive permeable material compatible with the system. The temperature of the cell may be maintained between about 0 and 40C., preferably between 25 and 35C. An emf of from 5 to l5 volts may be applied, preferably from 5 to 12 volts. The resulting anode current density may vary from 30 to. 100 ar'nperes, per square decimeter, preferably from 50 to 100. The electrochemical oxidation may be continued until the concentration of Na S O is between 200 and 950 g/l, preferably between 400 and 950 g/l.

The product 6 of the electrolytic cell 11 comprising a mixture of sodium bisulfate and sodium persulfate is divided into two streams. One stream is fed to the evaporator 5 for oxidation of the chloride ion inthe red liquor and the other stream is used to convert the trivalent chromium values to hexavalent values in the bisulfate solution 27 which is used to react with the yellow liquor 2.

According to a preferred method of the present invention, chromic anhydride is prepared by taking a portion of the crystalline sodium bichromate 20 produced in the crystallizer 17 passing it to a dissolving kettle 21 and there redissolving it in a quantity of water at a temperature of about 80C. to provide a solution having a concentration of about percent based on Na Cr O? The hot saturated solution is then crystallized in the dissolving vessel, or a separate crystallizer at a temperature of about l00-l40C. to crystallize out sodium bichromate anhydrous, Na Cr O 22. The filtrate 23 may be recycled to the multistage evaporator(s) 5. The anhydrous Na Cr o 22 is transferred to a conversion kettle 24 to which a sulfuric acid 25 is added with agitation to produce chromic anhydride (CrO and by-product NaHSO, (13). It is possible to eliminate the crystallization of the anhydrous sodium bichromate and add the sulfuric acid directly to the Na Cr O ZH Q, and drive off the water during the conversion step to CrO At the temperature employed, both the CrO 28 and the NaHSO, 13 are in liquid states, and are separated by one of the several methods of phase separation for immiscible liquids. Table 111 presents pertinent data on the preparation of chromic anhydride.

TABLE 111 Range Preferred Oleum SO 9 grams/gram Na cr o, 0.68 to 0.74 0.70 to 0.72 Temperature 197 to 203C. 197 to 200C. Time Required for conversion 0.5 to 1 hr. 0.5 to 1 hr.

The molten chromic anhydride 28 is transferred to a flaking roll and packaged as a saleable product 26.

The by-product sodium bisulfate 13 as NaHSO containing a small amount of water is transferred to an oxidizing vessel 29. This material, contaminated with trivalent chromium as well as decomposition products brought about by the high temperatures attained during the bichromate/chromic anhydride conversion, after cooling and some dilution with water is treated in vessel 29 with the second stream 6' of electrolytic cell product comprising sodium bisulfate and sodium persulfate. Table IV presents pertinent data concerning the oxidation of the trivalent chromium values.

TABLE IV Range Preferred of NaHSO in solution to 60% 50% to 60% grams Na S,O.,/gram Cr(lll) 6 to 9 gr. 7.0 to 8.5 gr. Temperature C. 60 to 115 60 to 70 Time 1.0 to 4.0 hrs. 1.5 to 3.0 hrs. pH 0 to 1 0 to 0.5

EXAMPLE 1 300 grams of a sodium bisulfate by-product contaminated with hexavalent and trivalent chromium and derived from a typical chromic anhydride manufacturing operation, is dissolved in 200 grams of water to form a solution containing 0.24 percent trivalent chromium (Cr Ill). The solution is heated to 60C. and treated with an electrochemical cell product containing 8.4 grams of sodium persulfate. The mixture is maintained at 60C. for 3 hours whereupon chemical analysis indicates that the Cr (111) content has decreased to 0.04 percent, corresponding to oxidation of about 83 percent of the trivalent chromium to hexavalent chromium. The method of analysis consists of a direct determination of the remaining trivalent chromium by precipitation as Cr(OH with ammonia followed by resolution in dilute sulfuric acid, oxidation by ceric sulfate, and titration of the hexavalent chromium thus formed with a standard sodium nitrite solution.

The thus treated sodium bisulfate is then combined at 80C. with a strong aqueous solution of sodium chromate (yellow liquor derived from roast leaching operations) containing about 540 grams of Na,CrO per liter and small amounts of residual Na,CO and NaCl from raw materials used in the process. The bisulfate and chromate solutions are combined in proportions to give a pH close to that of bichromate; that is, about 3.0. Thus, 234 grams of the bisulfate solution is treated as described above and 500 grams of the chromate solution produce 734 grams of a red liquor containing essentially sodium bichromate (174 grams as Na Cr o, 21-1 0) and sodium sulfate (166 grams as Na S0 along with a small amount of chloride ion (0.53 grams as NaCl). Some of the Na SO, in the red liquor system thus produced crystallizes out of solution at C.The mixture is evaporated to remove 321 grams of water, whereupon most of the remaining Na SO separates out and 240 grams of a liquor is obtained containing 168 grams of Na Cr O -2H 0, 0.63 grams'of Na S0 and 0.60 grams of NaCl. The liquor is treated for chloride removal by adding an electrochemical cell product containing 1.15 grams of sodium persulfate. The mixture is maintained at the boiling point (1 15C.) for one hour. During this period chlorine gas escapes from the system; chemical analysis indicates that the chloride content is reduced from 0.15% C1 to 0.05% Cl, corresponding to 67 percent removal of chloride ion under these conditions.

Final evaporation of the thus treated liquor causes separation of most of the remaining Na SQ, and yields a liquor containing about 83% Na Cr O -2l-l O by weight, which is a suitably purified feed for crystallization of the product Na Cr 0,-2H O.

- The sodium persulfate used to oxidize the Cr(lll) and the C1 is prepared by the electrochemical oxidation of a sample of by-product sodium sulfate derived from the bichromate-sulfate separation by combining 106.5 grams of by-product sodium sulfate with 73.4 grams of concentrated sulfuric acid and 270 grams of water to produce a solution containing 40 percent by weight NaHSO 200ml (267 grams) of this solution istransferred into a single-compartment electrochemical cell provided with a platinum anode of surface area 42 cm and platinum cathode of surface area 84- cm The latter is wrapped with asbestos cord which functions as a diaphragm to minimize cathodic reduction of per-- sulfate, yielding a cell product containing 191 grams/liter M3 5 0...

EXAMPLES 2 and 3 These examples illustrate the efficient removal of the chloride ion at abnormally high concentration levels.

A solution containing 750 grams Na Cr ofiH O, 500 grams H 0 and 27.4 grams NaCl is treated with 61.2 grams of sodium persulfate (10 percent in excess of the stoichiometric amount) and the mixture heated to 115C. for 100 minutes. At the end of this period,

the mixture contains only 0.005 Cl, corresponding to removal of over 99 percent of the chloride ion.

In another run, a slurry containing 350 grams N21 Cr O 2H O, grams H2O, grams and 50.0 grams NaCl,is treated with 112 grams of sodium persulfate 10 percent in excess of the stoichiometric amount), and the mixture heated to 118C. for minutes. At the end of this period the mixture contains only 0.015% Cl' corresponding to removal of 99.8% of the chloride.

EXAMPLE 4 NaHSO, Oxidation Temperature, C. Hours At 60C., 3 hours are required to oxidize 90 percent of the Cr(lll) to Cr(Vl), whereas at 70C. this is accomplished in one hour.

The novel series of steps comprising the method of the present invention constitute a substantial process improvement:

a. The troublesome brown muds encountered in those methods of the prior art which attempt to recover the acid values in the by-product bisulfate, have been eliminated.

b. Both the trivalent and hexavalent chromium values in the by-product bisulfate which were formerly lost with the brown muds are now recovered.

c. The troublesome filtration of the brown muds has been eliminated.

d. Disposal of the brown mud is no longer necessary. This is an important consideration, particularly in view of the pollution problem.

e. A second step in converting chromate to bichromate has been eliminated since the pH can be held at 3.0-3.5 rather than at 5.0, at which pH, filtration becomes possible, but completion of the conversion does not. At pH 3.0-3.5 complete conversion is obtained in one step.

f. Less evaporative equipment is required, which also represents a saving in fuel.

g. No foreign ions are introduced to complicate purification.

h. No additional raw material is required.

i. Less sulfuric acid is required than with most methods of the prior art. f

j. Chloride ion contamination is removed easily and efficiently.

While this invention has been described with reference to certain specific examples and illustrative embodiments, it is not intended that the application be thereby limited except insofar as it appears in the accompanying claims.

We claim:

1. A process for producing an alkali metal bichromate comprising roasting chrome ore under alkaline oxidation conditions at elevated temperatures to produce a roasted mixture, leaching said mixture with an aqueous solution to produce a liquor containing therein dissolved chrome values, acidifying said solution to a pH of less than 5 with an alkali metal bisulfate solution substantially free of trivalent chromium values at a temperature within the range of 25 to 120C. to convert the roasted mixture's chrome values at least in part to an alkali metal bichromate containing chloride impurities, adding an alkali metal persulfate to said alkali metal bichromate solution in an amount sufficient to oxidize contaminating chloride to chlorine, concentrating the bichromate solution by evaporation at temperatures within the range of 50 to 140C. driving off the chlorine and obtain a substantially chlorine-free alkali metal bichromate, and an alkali metal sulfate and recovering said alkali metal bichromate from said evaporated liquor.

2. The process of claim 1 wherein the alkali metal bichromate is sodium bichromate.

3. The process of claim 1 wherein the alkali metal bisulfate is sodium bisulfate.

4. The process of claim 1' wherein the alkali metal persulfate is sodium persulfate.

5. The method of claim 1 wherein the pH of the sodium chromate leach liquor is adjusted to between 3.0

and 3.5 by the addition of the bisulfate solution.

6. The process of claim 1 wherein the chrome ore is consisting of an alkali metal carbonate of sodium carbonate or potassium carbonate, calcium oxide and magnesium oxide.

7. The process of claim 1 wherein the roasting is conducted at temperatures within the range of 2,000 to 2,400F.

8. The process of claim 1 wherein the persulfate anions added to the chloride contaminated bichromate solution are produced by acidifying an aqueous alkali metal sulfate solution with at least the stoichiometric amount of a sulfuric acid necessary to convert the sulfate to bisulfate and converting the alkali metal bisulfate solution to an alkali metal persulfate solution by the electrochemical oxidation of the bisulfatesjolution in an electrolytic cell operated at a temperature of between about 0 to 40C., said oxidation being continued until the persulfate concentration of the solution reaches a strength of between about 200 and 950 grams/liter.

9. The process of claim 8 wherein the bisulfate concentration of the solution going to the electrolytic cell has an alkali metal bisulfate concentration of from about 40 to 60 percent by weight.

10. The process of claim 1 wherein the alkali metal persulfate is added to the alkali metal bichromate solution in a molar ratio of up to about 2 mols of alkali metal persulfate per mol of alkali metal bichromate.

11. The process of claim 1 wherein the alkali metal bisulfate solution substantially free of trivalent chromium values is produced by reacting under oxidation conditions an alkali metal persulfate with an alkali metal bisulfate contaminated with trivalentchromium in an amount sufficient to oxidize the trivalent chromium ions present in the bisulfate tothe hexavalent state and recovering the bisulfate substantially free of trivalent chromium values.

12. The method of claim 11 wherein the oxidation reaction is effected at a temperature between 60 and 13. The method of claim 11 wherein the oxidation of the bisulfate is continued until at least percent of the trivalent chromium has been oxidized to the hexavalent state.

14. The process of claim 11 wherein the ratio of persulfate to bisulfate is about 6 to 9 parts by weight persulfate per part of bisulfate.

15. A process of reducing the halide impurity content of an aqueous solution of an alkali metal bichromate which comprises reacting a sufficient amount of an alkali metal persulfate with said aqueous bichromate solution under reaction conditions sufficient to oxidize the halide to halogen, said conditions including maintaining said reaction solution at a pH within the range of about 3 to 5 and at a temperature from 50C. up to the boiling point of said aqueous solution, evolving halogen from said solution and recovering said bichromate solution of substantially reduced halide content.

16. The process of claim wherein the alkali metal bichromate is a sodium bichromate solution.

17. The process of claim 15 wherein the halide impu-- 

1. A process for producing an alkali metal bichromate comprising roasting chrome ore under alkaline oxidation conditions at elevated temperatures to produce a roasted mixture, leaching said mixture with an aqueous solution to produce a liquor containing therein dissolved chrome values, acidifying said solution to a pH of less than 5 with an alkali metal bisulfate solution substantially free of trivalent chromium values at a temperature within the range of 25* to 120*C. to convert the roasted mixture''s chrome values at least in part to an alkali metal bichromate containing chloride impurities, adding an alkali mEtal persulfate to said alkali metal bichromate solution in an amount sufficient to oxidize contaminating chloride to chlorine, concentrating the bichromate solution by evaporation at temperatures within the range of 50* to 140*C. driving off the chlorine and obtain a substantially chlorine-free alkali metal bichromate, and an alkali metal sulfate and recovering said alkali metal bichromate from said evaporated liquor.
 2. The process of claim 1 wherein the alkali metal bichromate is sodium bichromate.
 3. The process of claim 1 wherein the alkali metal bisulfate is sodium bisulfate.
 4. The process of claim 1 wherein the alkali metal persulfate is sodium persulfate.
 5. The method of claim 1 wherein the pH of the sodium chromate leach liquor is adjusted to between 3.0 and 3.5 by the addition of the bisulfate solution.
 6. The process of claim 1 wherein the chrome ore is mixed with alkaline materials selected from the group consisting of an alkali metal carbonate of sodium carbonate or potassium carbonate, calcium oxide and magnesium oxide.
 7. The process of claim 1 wherein the roasting is conducted at temperatures within the range of 2,000* to 2,400*F.
 8. The process of claim 1 wherein the persulfate anions added to the chloride contaminated bichromate solution are produced by acidifying an aqueous alkali metal sulfate solution with at least the stoichiometric amount of a sulfuric acid necessary to convert the sulfate to bisulfate and converting the alkali metal bisulfate solution to an alkali metal persulfate solution by the electrochemical oxidation of the bisulfate solution in an electrolytic cell operated at a temperature of between about 0* to 40*C., said oxidation being continued until the persulfate concentration of the solution reaches a strength of between about 200 and 950 grams/liter.
 9. The process of claim 8 wherein the bisulfate concentration of the solution going to the electrolytic cell has an alkali metal bisulfate concentration of from about 40 to 60 percent by weight.
 10. The process of claim 1 wherein the alkali metal persulfate is added to the alkali metal bichromate solution in a molar ratio of up to about 2 mols of alkali metal persulfate per mol of alkali metal bichromate.
 11. The process of claim 1 wherein the alkali metal bisulfate solution substantially free of trivalent chromium values is produced by reacting under oxidation conditions an alkali metal persulfate with an alkali metal bisulfate contaminated with trivalent chromium in an amount sufficient to oxidize the trivalent chromium ions present in the bisulfate to the hexavalent state and recovering the bisulfate substantially free of trivalent chromium values.
 12. The method of claim 11 wherein the oxidation reaction is effected at a temperature between 60* and 120*C.
 13. The method of claim 11 wherein the oxidation of the bisulfate is continued until at least 90 percent of the trivalent chromium has been oxidized to the hexavalent state.
 14. The process of claim 11 wherein the ratio of persulfate to bisulfate is about 6 to 9 parts by weight persulfate per part of bisulfate.
 15. A process of reducing the halide impurity content of an aqueous solution of an alkali metal bichromate which comprises reacting a sufficient amount of an alkali metal persulfate with said aqueous bichromate solution under reaction conditions sufficient to oxidize the halide to halogen, said conditions including maintaining said reaction solution at a pH within the range of about 3 to 5 and at a temperature from 50*C. up to the boiling point of said aqueous solution, evolving halogen from said solution and recovering said bichromate solution of substantially reduced halide content.
 16. The process of claim 15 wherein the alkali metal bichromate is a sodium bichromate solution.
 17. The process of claim 15 wheRein the halide impurity is a chloride.
 18. The process of claim 15 wherein the alkali metal persulfate is sodium persulfate.
 19. The process of claim 15 wherein the alkali metal persulfate is present in the reaction solution in a stoichiometric quantity sufficient to oxidize substantially all of the halide content of the bichromate solution to halogen. 